CN109563271A - By impregnating the method with vapor explosion treatment lignocellulose biomass - Google Patents
By impregnating the method with vapor explosion treatment lignocellulose biomass Download PDFInfo
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- CN109563271A CN109563271A CN201780044909.9A CN201780044909A CN109563271A CN 109563271 A CN109563271 A CN 109563271A CN 201780044909 A CN201780044909 A CN 201780044909A CN 109563271 A CN109563271 A CN 109563271A
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- biomass
- liquid
- zone
- dilvar zone
- dilvar
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- C—CHEMISTRY; METALLURGY
- C13—SUGAR INDUSTRY
- C13K—SACCHARIDES OBTAINED FROM NATURAL SOURCES OR BY HYDROLYSIS OF NATURALLY OCCURRING DISACCHARIDES, OLIGOSACCHARIDES OR POLYSACCHARIDES
- C13K1/00—Glucose; Glucose-containing syrups
- C13K1/02—Glucose; Glucose-containing syrups obtained by saccharification of cellulosic materials
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- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08H—DERIVATIVES OF NATURAL MACROMOLECULAR COMPOUNDS
- C08H8/00—Macromolecular compounds derived from lignocellulosic materials
Abstract
The present invention relates to the continuation methods that lignocellulose biomass is handled before enzyme hydrolysis, the method includes will be through broken, then the biomass through squeezing is transferred to the step of impregnating by acid solution, biomass through impregnating is dripped in the top in the region containing maceration extract, then gained wet biomass is squeezed and is sent to vapor explosion step.Before the explosion step, maceration extract is prepared by the used liquid from drippage operation and/or from extrusion operation in reserved area.The invention further relates to apparatus for implementing the method.
Description
Invention field
Method the present invention relates to processing lignocellulose biomass to produce the second generation (2G) syrup.These syrups are available
In via bio-chemical pathway generate other products (such as alcohols, such as ethyl alcohol, butanol or other molecules, such as solvent, such as
Acetone etc.).The method includes 3 steps, that is, prepare liquid, the dipping of biomass and pre-processed by vapor explosion through soaking
The biomass of stain.
The prior art
Lignocellulose biomass is one of the most abundant renewable resource on the earth.The substrate considered is very various
, they are both related to wood substrate, such as various timber (hardwood and cork), further relate to from agricultural by-product (cornstalk,
Corncob etc.) or by-product from industries such as other agricultural food products, papermaking.
Ligno-cellulosic materials are biologically converted into the method for 2G syrup particularly including pre-treatment step and are mixed via enzyme
The enzyme hydrolysis step that object (enzymatic cocktail) carries out.These methods normally also include the dipping step before pretreatment
Suddenly.Then the syrup generated by hydrolysis is for example handled by fermenting, and this method further includes separating step and/or final production
The purification step of object.
Lignocellulose biomass includes three kinds of principal polymerics: cellulose (35%-50%), be it is a kind of substantially by
The polysaccharide that hexose is constituted；Hemicellulose (20%-30%) is a kind of polysaccharide being substantially made of pentose；And lignin
(15%-25%) is a kind of polymer with labyrinth and high molecular weight, includes the aromatic alcohol connected by ehter bond.
These different molecules are responsible for the intrinsic characteristic of plant walls and themselves will be organized into complicated entanglement body.
In these three base polymers of composition lignocellulose biomass, cellulose and hemicellulose are able to produce 2G
Syrup.
In general, hemicellulose main decomposition saccharogenesis in preprocessing process, cellulose are converted into glucose by enzyme hydrolysis.
However, the acquisition of crude fibre is still difficult to enter enzyme wherein, it is therefore desirable to be pre-processed.The pretreatment allows to change
Become the physicochemical properties of ligno-cellulosic materials, the accessibility for entering cellulose so as to improve enzyme and cellulose are to enzyme hydrolysis
Reactivity.
Most effective pretreatment first is that vapor explosion, hemicellulose can be made almost to hydrolyze and significant
Improve accessibility and reactivity of the cellulose for enzyme.Its one or more elsewhere can be carried out before the pretreatment
Reason.
Patent US-8057639 and US-8512512 propose a kind of method comprising (thus prevent half in temperate condition
Cellulose is degraded) under make hydrolysis of hemicellulose to obtain the first step of C5 sugar.The step is in the first reactor 1.5
Bar or higher pressure under by injection vapor, under 110 DEG C or higher temperature and optionally in weak acid in the presence of into
Row.After this step, the remaining life that then will be enriched in cellulose and lignin to extract and recycle C5 syrup is washed
Substance is sent to the second step (second reactor) for wherein carrying out vapor explosion.The second reactor is in injection high-pressure steam
In the case where operated under pressure more higher than first reactor, this leads to the unexpected expansion (vapor explosion) of biomass.
Patent application US-2012/0104313 also proposed the processing step before vapor explosion, which passes through
Contact biomass at 100-210 DEG C 1 minute to 24 hours with water or vapor.Isolating the liquid phase rich in hemicellulose
And then solid is transferred to vapor explosion step.
Patent EP-2610346 describes a kind of method with 4 step process lignocellulose biomass: in 100-150
Liquid/solid is then demultiplex out in processing at a temperature of DEG C in a liquid, then by the solid portion of acquisition in water or vapor
In the presence of, pre-process 1 minute to 24 hours at 100-210 DEG C, finally terminated with liquid/solid separation.
Many patents, which are proposed through the dissolution of hemicellulose, improves pretreated various solutions, this leads to biology
Matter has preferably reactive in vapor explosion: dipping at high temperature, dipping under stress, in the presence of acid,
These steps are repeated under the same terms or different condition.
Patent application WO-2013/141776 is described in field of papermaking in the vertical means (leaching containing alkaline impregnation
Stain device) in dipping method, thus define the firstth area wherein impregnated.In the bottom reception lignocellulosic of infuser
Material shifts the top that screw rod transfers them to infuser by 2.Transferring them to the infuser being located above liquid level
During secondth area, biomass is drained and liquid drops back into the firstth area.In such construction, controlled by introducing lye
Liquid level.
In improved arrangement, from the bottom extracting liq of infuser, the top of infuser is filtered and then is recycled to
Portion, to generate the adverse current opposite with the direction of travel of biomass, this may be implemented that impurity (sand etc.) is discharged from biomass,
Otherwise the impurity can be deposited on the bottom of infuser.Liquid flows in the circuit for flowing through filtration system, and can add
Fresh liquid.
A kind of method is proposed in this application, and it uses infuser described in application WO-2013/141776, institutes
It states method and is suitable for the continuous industry scale use in the case where controlling operating condition.It is special with correlation unit according to the method for the present invention
The method that syrup or even alcohol Shi Yongyu do not produced by lignocellulose biomass.
The method of the prior art of this method than producing syrup field is simpler and cheaper.It is in moderate temperature and atmosphere
Pressing operation, and preferably with the operation of single impregnation steps.
Summary of the invention
More specifically, the processing lignocellulose biomass for being related to implementing before enzyme hydrolysis according to the method for the present invention is to produce
The continuation method of syrup, which comprises
1) ground biomass is transferred to the first transition range of the first Dilvar zone of impregnation steps, these described areas pass through anti-
Only liquid is separated from the biomass plug (plug) that first Dilvar zone flows upwardly to the transition range；
2) under atmospheric pressure two 10-95 DEG C at a temperature of the stacked Dilvar zone that operates in the impregnation steps implemented, it is raw
Residence time of the substance in the impregnation steps is -60 minutes 1 minute, and
First Dilvar zone receives the compacting biomass generated by the transition range, and the leaching containing the pH with 0.1-7
Stain liquid,
And
The biomass is transferred to the second Dilvar zone above first Dilvar zone, in second Dilvar zone
Drain the biomass through impregnating, to generate the gained wet biomass of the total solid content with 15wt%-40wt% and from institute
The liquid isolated in the first Dilvar zone is stated,
3) wet biomass is transferred to the second transition range of vapor explosion step,
Second transition range is in a chamber, on the one hand the chamber is separated with multiple Dilvar zones of the impregnation steps,
Multiple the separating out of another aspect and vapor explosion step,
The area of second Dilvar zone and the vapor explosion step is separated in a sealing fashion by biomass plug, and
In second transition range, squeeze the wet biomass so that the total solid content of biomass increase to 40 weight % or
More, and generate gained liquid,
4) vapor explosion step comprising:
By injection vapor by the cooking zone of biomass boiling 1-30 minutes, specific vapor consumption is
The biomass total solid into the area of 0.05-10 tons/ton, the cooking zone are in 150-250 DEG C of temperature and 0.5-
Under the pressure of 4MPa,
Followed by the breathing space for expanding the biomass generated by the cooking zone,
Followed by the Disengagement zone for separating vapor with biomass,
5) the step of preparing liquid using the liquid preparation facilities for being suitable for operating as follows:
Reception extracts from the second transition range and/or extracts from the liquid of the first Dilvar zone,
It is received as the acid and/or water of the value for making the pH of the inlet of the first Dilvar zone remain 0.1-7 and the input quantity of determination,
And wherein the liquid of the preparation is introduced into the first Dilvar zone.
Acronym " TS " is indicated according to standard ASTM E1756-08 (2015) " Standard Test Method
The total solid content of for Determination of Total Solids in Biomass " measurement.
Preferably, in the method according to the invention, the impregnation steps are implemented with single step.
Advantageously,
Implement the impregnation steps, described two Dilvar zones vertically and along the Dilvar zone that same axis is placed at two
It separates, so that liquid be allowed to flow to the firstth area from the secondth area, and stays the biomass in the second region, in the firstth area
Liquid level ensures that described two areas are spaced apart,
The biomass is transferred in second Dilvar zone from first Dilvar zone by screw rod.
Separate the liquid of a part from second Dilvar zone with the biomass through impregnating, it is preferable that make to come from
The liquid discharge (being separated by draining) of a part of the biomass through impregnating enters first Dilvar zone.
Preferably, liquid level is made to keep substantially constant by inputting acid solution.In general, the acid solution is only sulfuric acid solution.
Preferably, the acid solution has the pH of 0.1-2.
In an embodiment of the step of preparing the acid solution, described device receives the liquid for extracting from the second transition range
Body and the optional liquid for extracting from the first Dilvar zone.In a preferred embodiment, the step of preparing the acid solution connects
It receives the liquid from the first Dilvar zone and extracts from the liquid of the second transition range.
In general, the step of preparing liquid does not receive the liquid isolated in vapor explosion step or later.
In general, the cooking zone is horizontal tube reactor, and be provided with it is one or more by the biomass from upstream
Transition range be delivered to downstream breathing space screw rod.Term "horizontal", which is understood to refer to exist, is able to achieve the liquid flowing
Slight inclination.
Preferably, enzyme hydrolysis is carried out at least part of the biomass generated by the vapor explosion step, and obtained
Obtain syrup.
Preferably, alcoholic fermentation is carried out at least part of the syrup, generally produces ethyl alcohol.
The invention further relates to the unit of the continuous processing lignocellulose biomass before enzyme hydrolysis, the unit includes:
1) ground biomass is transferred to the first transition range of the first Dilvar zone of impregnation reactor under extrusion, it is described this
A little areas are separated by the biomass plug for preventing liquid from flowing upwardly to first transition range from first Dilvar zone；
2) include two stacked Dilvar zones impregnation reactor, wherein the second Dilvar zone is located at the top of the first Dilvar zone,
First Dilvar zone includes acid solution and is provided with entering for compacting biomass for being generated by first transition range
Mouth opening,
The reactor, which is provided with, is transferred to described second from the entrance opening in first Dilvar zone for the biomass
The screw rod of the exit opening of Dilvar zone,
The second Dilvar zone being located above the liquid of first Dilvar zone, second Dilvar zone are provided with one or more
Liquid is allowed to flow into first Dilvar zone from second Dilvar zone and wet biomass is made to stay in the sieve in secondth area,
3) wet biomass is transferred to the second transition range of vapor blast area under extrusion,
Second transition range is in a chamber, on the one hand the chamber is separated with the multiple Dilvar zone, on the other hand with
The vapor blast area separates,
Second Dilvar zone and vapor blast area are separated by suppressing biomass plug, to make the total of the biomass
Solid content increases to 40 weight % or more, and the plug prevents liquid from flowing upwardly to described second turn from the vapor blast area
Area is moved, and
Second transition range is provided with the pipeline in extrusion process extracting the waste liquid separated with wet biomass out,
4) include the vapor blast area that the biomass is displaced through to the screw rod in following continuous area:
Biomass cooking zone is provided with the pipeline and vapor of the compacting biomass that conveying is generated by second transition range
Pipeline is injected,
The breathing space for expanding the biomass generated by the cooking zone,
The Disengagement zone that vapor is separated with biomass,
5) acid solution prepares area, is provided with
The pipeline that blast area is delivered to from the waste liquid extracted out in the second transition range and/or conveying are extracted out from the first Dilvar zone
Waste liquid pipeline,
The pipeline of transport acid and/or the pipeline for conveying water,
The acid solution of the preparation is recycled to the pipeline of first Dilvar zone,
Stirring system and optional heating device.
Detailed description of the invention
It is the continuation method of the processing lignocellulose biomass before enzyme hydrolysis according to the method for the present invention.
It is integrated into the method for being intended to produce second generation sugar, and many bio-chemical pathways are it is possible thereby to obtain containing oxygen
Sub (such as alcohols, such as ethyl alcohol, butanol etc.).
Therefore, this application involves acid dip, then pass through the vapor explosion under the recycling and control of pickling bath liquor
Carry out pretreated integration method.
This method and production 2G sugar (i.e. by those of lignocellulose biomass acquisition) or widely biology base molecule
The method of (i.e. from natural substrates or from the molecule of natural substrates) is compatible.
Biomass and transition range
According to the difference of biomass (stalk, timber etc.), need to carry out grinding steps the technology hand so that particle size and step
Section is compatible with operating condition.For this purpose, simple cutting is enough, but fine or non-fine grinding may be needed.
In general, ground biomass has the at most particle size of 300mm (full-size).In general, using 5-100mm
Sieve implement the grinding of stalk, and by wood cutting at the width and 2- of length, 10-100mm with 20-160mm
The parallelepiped fragment of the thickness of 20mm.
Biomass through milling is delivered to the firstth area of impregnation steps via the first transition range.Advantageously, it is described these
Area is separated by biomass plug, the biomass plug prevent liquid from firstth area flow upwardly to the transition range or even into
One step is upper.
According to the present invention, the transition range under extrusion being described herein is provided with screw rod, is capable of forming sealing-plug
Conical compression area and the punch block for being optionally capable of forming liquid outlet.When processed biomass is with first less than 70%
When beginning TS content, the juice generated by biomass can be produced in the first transition range under the action of compression, it then can be only
It stands on and is transferred to the biomass of the first Dilvar zone to collect the juice.
Sealing screw rod or plug screw well known by persons skilled in the art are known as commonly used in a kind of means of this purpose
Screw rod.
The screw rod has conical section, and the conical section is connected to the bottom of the first Dilvar zone.Entering the first dipping
Before the entrance in area, biomass plug is generated in the end of the conical section.
Therefore, which serves both functions: on the one hand, biomass being introduced continuously into impregnation reactor, another party
Face, the upstream for forming plug to realize leakproofness and prevent liquid from leaking into from impregnation reactor screw rod and screw rod.
Impregnation steps
Atmospheric pressure and 10-95 DEG C at a temperature of implement the dipping.The residence time of biomass in the impregnation step is usually 1
- 60 minutes minutes, preferably at least 2 minutes, preferably at least 5 minutes, preferably up to 45 minutes are 2-35 minutes usual.Preferably, it
It is carried out with single step.
The step carries out in the impregnation reactor (or infuser) with tubular shape, and the reactor is vertical or opposite
In the angle inclined vertically less than 60 °.The reactor includes 2 stacked Dilvar zones being preferably placed in same axis.
Bottom zone is referred to as the first Dilvar zone and by the compacting biomass for receiving and being generated by the first transition range that is open.It is located above
Area (top region) is referred to as the second Dilvar zone, it receives the biomass generated by the first Dilvar zone.
The reactor (infuser) is provided with one or more screw rods, and the screw rod is by biomass via the first Dilvar zone
Bottom is transferred to the exit opening at the top by the second Dilvar zone.
First Dilvar zone (thus in the area wherein impregnated) corresponds to the space of impregnated liquid filling.Second Dilvar zone
Without Continuous Liquid Phase.The distribution kept constant between the first Dilvar zone and the second Dilvar zone is particularly advantageous.For this purpose, described
Reactor is preferably equipped with the system for adjusting liquid level equipped with detection system (liquid level sensor), and filling can be guaranteed to institute
The liquid level needed.
The maceration extract is the pH and 10-95 DEG C of temperature with 0.1-7.0, preferably 0.1-6 or more preferably 0.1-2
Aqueous solution.Acid is usually sulfuric acid.Such liquid is well known to those skilled in the art, and any commonly used in leaching
The acid of stain is all suitable.What the amount of acid and the temperature of liquid were usually fixed.Obtaining and keep the means of temperature is all ability
Known to field technique personnel.
Formed plug (shift screw rod at) during briquetting biomass and be filled with liquid the first Dilvar zone
Inlet decompression effect can preferably make biomass be saturated (sponge effect).Biomass is set to pass through the firstth area (the
Biomass is impregnated in one area) it is shifted towards the second Dilvar zone being located above liquid level.
In the second Dilvar zone, a part of maceration extract and being discharged during rising to the second Dilvar zone with warp
The biomass of dipping separates, and the liquid of discharge drops back into the first Dilvar zone.
Preferably, the second Dilvar zone makes wet biomass stay in the sieve in the second Dilvar zone, institute equipped with one or more
Therefore stating sieve allows liquid to flow into the first Dilvar zone from the second Dilvar zone.
When leaving the second Dilvar zone and impregnation reactor, the biomass for being impregnated and being drained is recovered and containing seldom
Or be free of free water.Its total solid content is usually 15 weight %-40 weight %.
The liquid isolated, commonly referred to as waste liquid are present in the liquid of the first Dilvar zone.
The pipeline for the liquid that the infuser is generated equipped with one or more conveying by liquid preparation area, is further equipped with one
The pipeline of item or a plurality of extraction liquid.The suction line and outlet line of the liquid are usually mounted on first in the opposite manner
Between the bottom and top of Dilvar zone, this may be implemented to be operated in the case where cocurrent or countercurrent recycles.
The preparation of maceration extract
Due to dipping, there are the losses of liquid and acidity.It is therefore desirable to regularly add fresh acid solution.
These additions can accurately adjust the liquid level in impregnation reactor.
The step of preparation of liquid is also its adjustable operating parameter (such as temperature, pH or any other characteristic).It is logical
The input of peracid and/or water adjusts acid concentration appropriate.
It can also generate uniform liquid.
The step carries out in liquid preparation area.
Various devices, such as blending tank or mixer (preferably static mixer) equipped with stirring system can be used.
Preferably, sensor of the described device equipped with the flow of measurement pH and water, acid, waste liquid and the liquid of preparation etc..
The control for balanced flow and acidity can be implemented in all these sensors, to realize steady at desired conditions
Fixed continuous operation.
Be equipped with liquid preparation facilities and/or infuser, be located at beside described device (tank, mixer etc.) with to will pass through or
The collet, coil and/or heat exchanger that (described below) directly on such devices is recirculated back to road are heated.
The device for being used to prepare liquid is connected to infuser by the pipeline of one or more conveying liquid.
It is therefore possible to use can obtain determining pH (or any other characteristic) concentration appropriate and flow appropriate
Liquid is prepared, can be the setting value etc. for control.Control well known by persons skilled in the art will not be described in detail further
Means.
In general, acid solution prepare area equipped with:
The waste liquid extracted out from the second transition range is delivered to the pipeline of vapor blast area and/or conveyed from the first Dilvar zone and is taken out
The pipeline of waste liquid out,
The pipeline of transport acid and/or the pipeline for conveying water
The acid solution of the preparation is recycled to the pipeline of the first Dilvar zone,
Stirring system and optional heating device.
The example of recirculation circuit is as shown below.
Referred to as single recirculation circuit of circulating reflux recirculation circuit
Liquid recirculation loops can be advantageously arranged in around the firstth area of impregnation steps, and it is commonly known as recycled
Reflux circuit, because this is the problem of extracting out and recycle in same area.
There is a possibility that two kinds of re-injections: cocurrent (inject in bottom and extracted out at top) or adverse current (top inject and
Bottom extraction).The circuit allows to liquid with better uniformity and stability, connects liquid preferably with biomass
Touching, can also adjust the liquid level of the first Dilvar zone.
Preferably, after separating Biomass, liquid is extracted out at the liquid level close to the first Dilvar zone.The liquid is at it
It is extracted out at the high position of middle liquid waste concentration, so that preparing the characteristic that Qu Zhongqi characteristic is adjusted to fresh liquid in liquid.
Before waste liquid return, waste liquid is especially set to flow through liquid preparation step, in this step in the proper ratio to it
Middle addition acid and/or water.
Such arrangement can improve the uniformity of the liquid in the first Dilvar zone significantly, make between biomass and liquid
With more effective contact and can in the firstth area temperature with higher.In this case, its advantage is that reducing
Difference between fresh liquid and the characteristic of waste liquid.
Into preparation step liquid characteristic by (pH, flow etc.) sensor measurement, and water to be added and/
Or the amount of acid is determined by control system to reach setting value, such as the pH to be recycled to the liquid in the first Dilvar zone.
Following attached drawing is described using the following drawings label:
Fig. 1: single cycle reflux (cocurrent) recycling
1: ground biomass
2: the first transition ranges/step
3a: infuser, the firstth area
3b: infuser, the secondth area
5: liquid of the extraction to be recycled for cocurrent circulating reflux from infuser
4: the liquid in injection infuser to be recycled for cocurrent circulating reflux
6: liquid preparation facilities (tank)
7: into the supplement water of liquid preparation tank
8: into the supplemental acid of liquid preparation tank
9: the second transition ranges/step
10: the downstream (passing through the pretreatment of vapor explosion) of dipping process.
Fig. 2: in the single recycling after extruding of dipping downstream
1: ground biomass
2: the first transition ranges/step
3a: infuser, the firstth area
3b: infuser, the secondth area
4: the liquid in injection infuser to be recycled for cocurrent circulating reflux
6: liquid preparation tank
7: into the pipeline of the supplement water of liquid preparation tank
8: into the pipeline of the supplemental acid of liquid preparation tank
9: the second transition ranges/step
10: the downstream (passing through the pretreatment of vapor explosion) of dipping process
11: after impregnating by squeezing the liquid (extrusion liquid) extracted out from the second transition range.
Fig. 3: Two-way Cycle flows back (cocurrent) and extrusion liquid recycling
1: ground biomass
2: the first transition ranges/step
3a: infuser, the firstth area
3b: infuser, the secondth area
4: the liquid in injection infuser to be recycled for cocurrent circulating reflux
5: liquid of the extraction to be recycled for cocurrent circulating reflux from infuser
6: liquid preparation tank
7: into the supplement water of liquid preparation tank
8: into the pipeline of the supplemental acid of liquid preparation tank
9: the second transition ranges/step
10: the downstream (passing through the pretreatment of vapor explosion) of dipping process
11: after impregnating by squeezing the liquid (extrusion liquid) extracted out from the second transition range.
Fig. 1 illustrates the operation in the circuit.
Ground biomass is introduced into this method via pipeline 1 and shifts (the first transition range 2) into infuser 3, more
It is specifically transferred in the first Dilvar zone 3a of infuser.The area includes the liquid conveyed by pipeline 4, and the liquid is by liquid system
Standby device (step) 6 generates.The device 6 receives the second Dilvar zone 3b from infuser via pipeline 5 and divides with biomass
From liquid, and the device 6 be provided be respectively used to addition water and acid pipeline 7 and pipeline 8.It will be obtained after isolating liquid
Wet biomass be transferred to the next step of this method from the second transition range 9, the step be usually pass through vapor explosion into
The pretreated step of row, such as carried out in area 10.
Using other one or more downstream liquidsMaterialSingle recirculation circuit of stream
It is isolated after impregnation steps (or after infuser), more specifically after the second Dilvar zone of the step
Other liquid streams can also be after flowing through liquid preparation step (device) as dipping recycling.Advantageously, will be described
Stream introduces before preparation step, passes through the characteristic of stream described in (flow, pH's etc.) sensor measurement.Control to the device
It may be implemented to add water and/or acid with correct ratio, to prepare the liquid with appropriate characteristics.Preferably, the stream is
Extrusion liquid (liquid that the second transition range by wet biomass to be transferred to vapor explosion step generates).In fact, the stream
It is the waste liquid still containing acid, therefore it is recyclable.
The operation that the liquid recycle in downstream will be impregnated is following (referring to Fig. 2): when appended drawing reference is identical, will not be repeated again
For description and appended drawing reference made by Fig. 1.
In Fig. 2, extrusion liquid is transported to liquid preparation step by pipeline 11.The extrusion liquid (is used for by the second transition range 9
Wet biomass is transferred to vapor blast area) it generates.
However, in this arrangement of Fig. 2, the waste liquid separated in the second Dilvar zone of infuser with biomass no longer by
It is sent in liquid preparation step.
When the fresh liquid for entering the firstth area and in the form of extrusion liquid (or more generally in the form of other streams) and biomass
Between isolated waste liquid almost without when difference, it is preferable to use this arrangement.
The recirculation circuit of referred to as double recirculation circuits
It is by the recirculation circuit combination of front two, to be benefited from a combination thereof advantage.
Fig. 3 illustrates the operation of double recycling.For identical appended drawing reference, it will not be repeated again identical earlier drawings
Description.
Therefore, in Fig. 1 and Fig. 3, the waste liquid 5 of the first Dilvar zone of infuser is formed back and flowing through liquid and preparing area
Road.The recycling can occur with the circulation cocurrent or countercurrent of biomass in the first Dilvar zone of infuser.
Similarly, downstream liquid 11 (such as the extrusion liquid generated by the second transition range) is sent to preparation area.Therefore, liquid
Preparation area receive two kinds (or more) waste liquid and be mixed.
Sensor described above sends information necessary to the determination suitable water to be added and acid, has leaching to obtain
The recycled liquid of pH and flow needed for firstth area of stain device.
According to the present invention, therefore liquid preparation step can be implemented in various ways:
In the first Dilvar zone from infuser extraction liquid and by liquid recycle to infuser；
Extraction is located at one or more liquid (such as extrusion liquid) in dipping downstream and is recycled to the first dipping of infuser
Qu Zhong；This arrangement is advantageous, in the case where property difference very little especially between downstream liquid and fresh liquid,
Using double recycling, i.e., in the first Dilvar zone from infuser extraction liquid and by liquid recycle to infuser, also
Extraction is located at one or more liquid in dipping downstream and is recycled in the first Dilvar zone of infuser.This arrangement is extensive
Preferably.
It is transferred to the area of vapor explosion step under extrusion
Vapor explosion is successively transferred to via the second transition range by the wet biomass that the second Dilvar zone of impregnation steps generates
Step.
Second transition range is separated with Dilvar zone, and one or the other the second transition range not being arranged in Dilvar zone
Chamber in.For example, transition range is located at infuser in the case where including the infuser in 2 areas (Dilvar zone and drain area)
It is external.
Second transition range is also separated with vapor blast area.
By with biomass is transported to impregnation steps the first transition range in it is identical in a manner of, the second Dilvar zone and wherein send out
The reactor of unboiled water steam explosion step is separated by biomass plug.The plug prevents liquid from vapor blast area
One area flows upwardly to transition range or even further upper.
In the second transition range between second Dilvar zone of impregnation steps and the firstth area of vapor explosion step
Ensure the leakproofness.
A kind of means commonly used in this purpose are the screw rods of plug screw referred to as well known by persons skilled in the art.Herein
The conical section of screw rod is connected to the first vapor blast area.Non-tapered section is connected to second Dilvar zone.
The formation of biomass plug ensures the leakproofness of the pressure for vapor explosion reactor, to prevent water
The dangerous evolution of steam.
In second transition range, wet biomass is squeezed to increase the TS content of biomass.Biomass obtained
Total solid content is generally at least 40 weight %, preferably greater than 40 weight %, even more preferably 40 weight %-70 weight %.
Second transition range is additionally provided with for (referred to as squeezing the waste liquid separated with wet biomass during extruding
Liquid out) extraction pipeline.
As described above, waste liquid is advantageously recirculated in impregnation steps.
It should be noted that the biomass drained is before hydrolysis without being intended to reduce the mechanical treatment of size.
The vapor explosion step carried out in vapor blast area
It is generallyd use:
Cooking zone, wherein contact biomass and vapor 1-30 minute, specific vapor consumption for 0.05-10 tons/
The biomass total solid of ton, the area are under 150-250 DEG C of temperature and the pressure of 0.5-4 MPa,
Followed by make the breathing space of biomass expansion generated by cooking zone,
Followed by the Disengagement zone for separating vapor with biomass.
The vapor of recycling is advantageously recirculated to vapor explosion step upon compression, or is optionally recycled to existing
In the public utility of field.
Preferably, tubular reactor of the step at horizontal (that is, it can be tilted so that liquid flows) very slightly
Middle progress.
Biomass cooking zone is provided with the pipeline for the compacting biomass that conveying is generated by the second transition range and vapor injects
Pipeline.Boiling carries out at high temperatures and pressures.Implement to pressurize by injection vapor, to reach the pressure of 0.5-4MPa.It steams
Boiling temperature is usually 150-250 DEG C.Preferably, adjusting condition is so that digestion time is limited in 1-30 minutes.
The step is using the reactor for being provided with screw rod, and the screw rod is for making biomass be displaced through continuous area.Institute
Stating screw rod ensures continuously to convey biomass, and the speed of adjusting screw rod is to meet residence-time conditions.
In the end (in the end of reactor) of screw rod, biomass in the pipeline for being known as spurting pipeline by vapor very
It is rapidly entrained to breathing space, the pipeline has reduced diameter relative to cooking zone.
Breathing space includes pipeline, wherein biomass circulating and cross section limiting member is flowed through, then after removing the limitation
Expansion suddenly.
Pipeline is spurted with cross section limiting member, can be the hole for allowing small flow area or there is adjustable open
The valve (such as diaphragm valve) of mouth.Under this limitation, biomass is reached with very high travelling speed, and is undergone quick and big
Then pressure change expands suddenly after removing the limitation, this destroys the biomass through boiling.This is why it is claimed
The reason of for vapor explosion.
The limitation defines vapor flow and thus defines specific vapor consumption (vapor flow/dry life
Mass flow-rate).In general, the specific vapor consumption is 0.05-10 tons/ton total solid.
Once flowing through breathing space, biomass is carried secretly by vapor and (or returns to and limiting than limiting bigger diameter across having
The diameter of upstream processed) and biomass is transported to the pipeline that spurts for being used for area for example via cyclone separator separation vapor
Rest part.
There is abundant accessibility of the cellulose for enzyme by the biomass through explosion that Disengagement zone generates now, with
It is handled by enzyme hydrolysis to generate 2G sugar.
The condition of enzyme hydrolysis and continuous or spontaneous fermentation is suitable for required product, and is known to those skilled in the art
's.
Second is prepared in the method by lignocellulose biomass preparation sugar and by the syrup according to the method for the present invention
Particularly advantageous application is had found in the method for alcohol.
Such method is known.Method by lignocellulose biomass preparation sugar includes pretreatment, advantageously
It is vapor explosion, followed by enzyme hydrolysis.Method by sugar production ethyl alcohol further includes the alcoholic fermentation of the sugar.
In the method according to the invention, enzyme is carried out at least part of the biomass generated by vapor explosion step
Hydrolysis, and obtain syrup.Preferably, the biomass is introduced to enzymatic hydrolysis reaction device in the case where no intermediate mechanical step
In.
In the method according to the invention, enzyme is carried out at least part of the biomass generated by vapor explosion step
Hydrolysis obtains syrup and carries out alcoholic fermentation at least part of the syrup.
Embodiment
In the embodiment being described below, acronym " TS " is indicated according to standard ASTM E1756-08 (2015)
" Standard Test Method for Determination of Total Solids in Biomass " is measured total solid
Content.
Embodiment 1 (comparison)
In the embodiment 1, the biomass of processing is stalk ground on 50mm sieve in advance.Ground stalk has
The xylose that the TS of the TS glucose content and every 100g that are estimated as 39.9g of 90.2% TS, every 100g is estimated as 26.6g contains
Amount.
Stalk is handled according to method of the invention is not met.
In the first step, ground stalk is contacted with the acid solution for being previously heated to 70 DEG C 4 hours.Contact
It operates (dipping of liquid) to carry out in the following manner with the mode of interval: capacity 1m3Tank it is ground filled with 62.1kg
Stalk (i.e. 56kgTS), then sieve is arranged on ground stalk and using the pressure of the counterweight of 4 each 2kg.Then
By the H containing 4.72kg of 685kg2SO4Acid and surplus are that the acid solution of water is introduced into tank.After contact 4 hours, arranged by gravity
It is dry to empty the tank.The average magnitude of extracting solution is 469kg.Then the biomass drained is transferred in buffering hopper, is then fallen
On a moving belt, it is finally introducing in cone-type spiral conveyer, pansman is continuously fed to the average flow rate of 203.2kg/h
Tool.In order to keep feed rate, one tank of preparation in every 82 minutes.During passing through in cone-type spiral conveyer, life is formed
Substance plug, which ensure that the leakproofness for the digestion reactors being maintained at 190 DEG C.With the flow of average 133.6kg/h, boring
In shape screw conveyor in the compression process of biomass from biomass extracting liq.By with the mean flow of 384.7kg/h
Vapor, which is added, in amount makes digestion reactors be maintained at 190 DEG C.When leaving reactor, by biomass fast decompression and in atmospheric pressure
Under be collected into tank.In transfer process between digestion reactors and collecting tank, make in cyclone separator pretreated
Substrate is separated with gas phase.The collection flow of such pretreated biomass is 85.5kg/h.Its TS is measured as 40.7%.It will revolve
The steam condensation isolated at the top of wind separator, and condensate is collected with the average flow rate of 368.8kg/h.
Pretreated biomass has the potential Xylose Content of 20.2g/100g TS, and 17.5g/100g TS therein is
The form of xylose monomers and soluble oligomer.
Therefore, xylose surplus shows 91.3% conversion ratio of the xylose that initially there are.
The method for not meeting the embodiment of the present invention 1 needs consumption (TS relative to 1kg processing) in detail below
Water: 12.14kg water/kg processing TS
Sulfuric acid: the TS of 84.3g/kg processing
Vapor: the TS of 9.4 kg/kg processing.
In addition, the method for embodiment 1 has sizable equipment requirement: the minimum volume of contact is 2.2m3.In order to fill
Contact tank and the volume pumped is about 0.5m3/h。
Embodiment 2 (according to the present invention)
In example 2, the biomass of processing is stalk same as Example 1.By ground biomass with 45.4kg/h
Average flow rate be introduced into immersion tool via the first transition range, by the compressed biomass in the first transition range.It will be through pressing
The biomass of contracting is introduced into the immersion tool with 2 meters of working depth, and there are two can be with 106m/ for immersion tool outfit
The parallel screw of the equivalent linear velocity vertical transport biomass of h.The total working volume of immersion tool is 78 liters, the first Dilvar zone
The volume in (referred to as submergence area) is 45 liters.Below liquid level at 5cm, the acid solution of 412kg/h is added, the acid solution is by preparing the liquid
The area of body generates.The temperature of the acid solution of injection is 80 DEG C.Therefore, in the first Dilvar zone, contact biomass with acid solution.First
Mean temperature in Dilvar zone is 73.5 DEG C.
At the bottom of immersion tool, liquid (waste liquid) is extracted out with the flow of 232.1kg/h.According to the present invention, the liquid
It is sent back to liquid preparation area.Biomass through impregnating is left by the top of impregnation reactor with the flow of 225.3kg/h.
Therefore, three kinds of streams are conveyed into the area of preparation acid solution: the waste liquid extracted out from immersion tool is (with 232.1kg/h's
Flow), with the sulfuric acid (being expressed as 100 weight % equivalents) of the flow of 2.52kg/h and with the water of the flow of 177.4kg/h.By this
It is a little to be mixed in the agitator tank with 560 liters of unit volume into stream, the liquid of preparation is extracted out (with the stream of 412kg/h
Amount), it send to heat exchanger and is heated to 80 DEG C of temperature, then as described above in injection immersion tool.
Then it will be conveyed on tape using the stalk of acid solution dipping, be then transferred to steaming via transition range in conical screw
It boils in tool.In the transfer process, liquid (waste liquid) is with the traffic flow of 127.8kg/h.
In digestion reactors, vapor is injected with the flow of 347kg/h.Vapor injection allows to reactor
Temperature be maintained at 190 DEG C.When leaving reactor, by biomass fast decompression and collect in tank under atmospheric pressure.It is steaming
It boils in the transfer process between reactor and collecting tank, separates pretreated substrate with gas phase.Such as
The collection flow of this pretreated substrate is 92.8kg/h.Its TS is measured as 38.5%.It will be separated at the top of cyclone separator
Steam out is condensed to generate condensate, condensate flow 351.8kg/h.
Pretreated substrate has the potential Xylose Content of 19.8g/100g TS, and 17.3g/100g TS therein is wood
The form of sugar monomer and soluble oligomer.Therefore, xylose surplus shows 91.7% conversion ratio of the xylose that initially there are.
The method of embodiment according to the present invention 2 needs consumption (TS relative to 1kg processing) in detail below
Water: 4.34kg water/kg processing TS
Sulfuric acid: the TS of 61.5g/kg processing
Vapor: the TS of 8.5 kg/kg processing.
Therefore, degree same as Example 1 can be realized in pre-treatment step according to the method for the invention of embodiment 2
Xylose, while ensure to reduce significantly water and acid consumption, make respectively water consumption reduce by 64%, make acid disappear
Consumption reduces by 27%.
In addition, the method for embodiment 2 has reduced equipment requirement: the minimum volume for acid solution dipping is less than 1m3, packet
Including including liquid preparation tank and immersion tool.Volume to be pumped around dipping pumping and extraction liquid is about 0.6m3/h。
Embodiment 3 (according to the present invention)
Embodiment 3 uses the poplar of the form of chips of the average-size with 50mm long and 10mm thickness as biomass, initial
TS content is 55.7%.Before treatment, biomass is made to be in environment temperature, i.e., at about 20 DEG C.
Biomass is introduced into dipping work same as Example 2 via the first transition range with the average flow rate of 140.2kg/h
In tool.Compressed biomass is introduced into the immersion tool with 2 meters of working depth, there are two energy for immersion tool outfit
The parallel screw of enough equivalent linear velocity vertical transport biomass with 106m/h.In the bottom of immersion tool, 163.9kg/h is added
Acid solution, the acid solution by preparation area generate.The temperature of the acid solution of injection is 80 DEG C.Therefore, in the first Dilvar zone, make biomass
It is contacted with acid solution.Mean temperature in first Dilvar zone is 55.9 DEG C.When leaving immersion tool, mentioned with the flow of 304kg/h
It learns from else's experience the biomass of dipping.According to standard ASTM E1756, measuring its TS is 27.1%TS.
Then the biomass through impregnating is conveyed on tape, pansman is then transferred to by transition range in conical screw
In tool.In the transfer process, liquid (acid pickle) is with the traffic flow of 161.7kg/h.According to the present invention, it is known as squeezing by this
The liquid of liquid is collected and is pumped into acid solution preparation area out.In digestion reactors, vapor is injected with the flow of 416.9kg/h.
Vapor injection can make the temperature and pressure of reactor be kept at 200 DEG C and 1.49MPa.Leaving digestion reactors
When, by biomass fast decompression and collect in tank under atmospheric pressure.Transfer process between digestion reactors and collecting tank
In, separate pretreated substrate with gas phase.The collection flow of such pretreated substrate is
145.9kg/h.Its TS is measured as 49.9%.The steam isolated at the top of cyclone separator is condensed, is to generate flow
The condensate of about 413.3kg/h.
The extrusion liquid extracted from the second transition range for being used to be transferred to digestion reactors is sent to liquid preparation area.The area by
Blending tank and heat exchanger composition.Blending tank makes up line by water, dense H2SO4Solution makes up line and conveys the extrusion liquid of recycling
Pipeline supply, and have for extract prepare liquid pipeline.Heat exchanger is placed on the liquid line of preparation (from mixed
Close tank and march to infuser) on, so as to reheat the liquid for leaving tank, and control the temperature for introducing the liquid of immersion tool
Degree, it is unrelated with blending tank and its temperature of input.In used construction, water and H2SO4(100%) magnitude of recruitment is respectively
1.2kg/h and 1kg/h.The outlet temperature of the heat exchanger of acid solution is 80 DEG C.Therefore, implementation according to the method for the present invention is so that can
To handle timber with the consumption of the acid of minimum and water.The TS that the specific consumption of acid enters for 12.8g/kg, and water
Specific consumption be 15.4g/kg TS.
Embodiment 4 (according to the present invention)
Embodiment 4 handles poplar same as Example 3.Therefore, this method processing rated flow is having for 140.2kg/h
The poplar of the form of chips of the average-size of 50mm long and 10mm thickness, initial TS content are 55.7%, and before treatment
It is stored at a temperature of 20 DEG C.Biomass is introduced into immersion tool same as Example 2 via the first transition range.It will be through pressing
The biomass of contracting is introduced into the immersion tool with 2 meters of working depth, and there are two can be with 106m/h for immersion tool outfit
Equivalent linear velocity vertical transport biomass parallel screw.In the bottom of immersion tool, the acid solution of 570kg/h is added, the acid
Liquid is generated by liquid preparation area.The temperature of the acid solution of injection is 80 DEG C.Therefore, in immersion tool, make transfer biomass with
Acid solution contact.Below liquid level at 15cm, waste liquid is extracted out with the flow of 407kg/h.According to the present invention, which is sent to liquid
Prepare area.
Mean temperature in first Dilvar zone is 70.1 DEG C.When leaving immersion tool, extracted with the flow of 303.1kg/h
Biomass through impregnating.According to standard ASTM E1756, measuring its TS is 27.2%.
Then the biomass through impregnating is conveyed on tape, pansman is then transferred to by transition range in conical screw
In tool.In the transfer process, liquid (waste liquid) is with the traffic flow of 161.7kg/h.This liquid for being known as extrusion liquid is received
Collect and is pumped into acid solution preparation area.In digestion reactors, vapor is injected with the flow of 414.2kg/h.Vapor injection
The temperature and pressure of reactor can be made to be kept at 200 DEG C and 1.49MPa.When leaving digestion reactors, by biomass
Fast decompression is simultaneously collected in tank under atmospheric pressure.In transfer process between digestion reactors and collecting tank, in whirlwind point
From separating pretreated biomass with gas phase.The collection flow of pretreated biomass is 142.5kg/h.Its TS
It is measured as 51.1%.The steam isolated at the top of cyclone separator is condensed, to generate flow as the condensation of 413.1kg/h
Object.
According to the present invention, the extrusion liquid extracted from the second transition range for being used to be transferred to digestion reactors is sent to liquid system
Preparation area.The area is made of blending tank and heat exchanger.Blending tank makes up line by water, dense H2SO4Solution makes up line, conveys and follow again
The pipeline supply for the liquid that the pipeline of the extrusion liquid of ring and conveying are extracted out from the first Dilvar zone.The tank also has for the system of extracting out
The pipeline of standby liquid.The content of blending tank is maintained at 1100kg.Heat exchanger is placed on the liquid line of preparation (from mixing
Tank marches to infuser) on, so as to reheat the liquid for leaving tank, and control the temperature for introducing the liquid of immersion tool
Degree, it is unrelated with blending tank and its temperature of input.In used construction, water and H2SO4Magnitude of recruitment be respectively 1.2kg/h
And 1kg/h.The outlet temperature of the heat exchanger of acid solution is 80 DEG C.
Therefore, the waste liquid in the first Dilvar zone is extracted out and extrusion liquid is extracted out and is recycled into liquid preparation tank
Setting can by the temperature of the first Dilvar zone improve 14.2 DEG C, while keep heating prepare liquid temperature at 80 DEG C,
It is lower than the bubble point of the liquid.
Claims (14)
1. the processing lignocellulose biomass implemented before enzyme hydrolysis is to produce the continuation method of syrup, the method packet
It includes:
1) ground biomass is transferred to the first transition range of the first Dilvar zone of impregnation steps, these described areas pass through anti-
Only liquid is separated from the biomass plug that first Dilvar zone flows upwardly to first transition range,
2) under atmospheric pressure two 10-95 DEG C at a temperature of the stacked Dilvar zone that operates in the impregnation steps implemented, it is raw
Residence time of the substance in the step is -60 minutes 1 minute, and
First Dilvar zone receives the compacting biomass generated by the first transition range, and the leaching containing the pH with 0.1-7
Stain liquid,
And
The biomass is transferred to the second Dilvar zone above first Dilvar zone, in second Dilvar zone
Drain the biomass through impregnating, to generate gained wet biomass and the separation of the total solid content with 15wt%-40wt%
Liquid,
3) wet biomass is transferred to the second transition range of vapor explosion step,
Second transition range is in a chamber, on the one hand the chamber is separated with multiple Dilvar zones of the impregnation steps,
On the other hand it is separated out with the multiple of vapor explosion step,
Second Dilvar zone and the reactor of vapor explosion step are separated in a sealing fashion by biomass plug, and
In second transition range, squeeze the wet biomass so that the total solid content of biomass increase to 40 weight % or
More, and generate gained liquid,
4) vapor explosion step comprising:
By injection vapor by the cooking zone of biomass boiling 1-30 minutes, specific vapor consumption is
The biomass total solid into the area of 0.05-10 tons/ton, the cooking zone are in 150-250 DEG C of temperature and 0.5-
Under the pressure of 4MPa,
Followed by the breathing space for expanding the biomass generated by the cooking zone,
Followed by the Disengagement zone for separating vapor with biomass,
5) the step of preparing liquid using the preparation facilities for being suitable for operating as follows:
Reception extracts from the second transition range and/or the liquid from the first Dilvar zone,
It is received as the acid and/or water of the value for making the pH of the inlet of the first Dilvar zone remain 0.1-7 and the input quantity of determination,
Wherein the liquid of the preparation is introduced into the first Dilvar zone.
2. the method as described in claim 1, wherein the impregnation steps are implemented with single step.
3. method as described in any one of the preceding claims, in which:
Implement the impregnation steps, described two Dilvar zones vertically and along the Dilvar zone that same axis is placed at two
It separates, so that liquid be allowed to flow to the first Dilvar zone from the secondth area, and stays in the biomass in the second Dilvar zone, the
Liquid level in one Dilvar zone ensures that described two areas are spaced apart,
The biomass is transferred in second Dilvar zone from first Dilvar zone by screw rod.
4. method as described in any one of the preceding claims, wherein making liquid level keep substantially constant by inputting acid solution.
5. method as described in any one of the preceding claims, wherein the acid solution is only sulfuric acid solution.
6. method as described in any one of the preceding claims, wherein the acid solution has the pH of 0.1-2.
7. method as described in any one of the preceding claims, wherein the reception of the step of preparation acid solution extracts from second turn
The liquid in shifting area is with optional from the liquid from the first Dilvar zone.
8. method as described in any one of the preceding claims, wherein the step of preparation acid solution is received from the first dipping
The liquid in area and the optional liquid for extracting from the second transition range.
9. method as described in any one of the preceding claims, wherein in second transition range of transfer wet biomass,
The total solid content of biomass after extrusion is 40 weight %-70 weight %, and preferably greater than 40 weight %.
10. method as described in any one of the preceding claims wherein the cooking zone is horizontal tube reactor, and is arranged
There is the screw rod of one or more breathing spaces that the biomass is delivered to downstream from the second transition range of upstream.
11. method as described in any one of the preceding claims, wherein the ground biomass is at most 300mm's
Size.
12. method as described in any one of the preceding claims, wherein to the biology generated by the vapor explosion step
At least part of matter carries out enzyme hydrolysis, and obtains syrup.
13. method as claimed in claim 12, wherein at least part to the syrup carries out alcoholic fermentation.
14. the unit of continuous processing lignocellulose biomass before enzyme hydrolysis, the unit include:
1) ground biomass is transferred to the first transition range of the first Dilvar zone of impregnation reactor under extrusion, it is described this
A little areas are separated by the biomass plug for preventing liquid from flowing upwardly to first transition range from first Dilvar zone,
2) include two stacked Dilvar zones impregnation reactor, the second Dilvar zone is located at the top of the first Dilvar zone,
First Dilvar zone includes acid solution and is provided with entering for compacting biomass for being generated by first transition range
Mouth opening,
The reactor be provided with the biomass be transferred to from the entrance opening in first Dilvar zone it is described
The screw rod of the exit opening of second Dilvar zone,
The second Dilvar zone being located above the liquid of first Dilvar zone, second Dilvar zone are provided with one or more
Liquid is allowed to flow into first Dilvar zone from second Dilvar zone and wet biomass is made to stay in the sieve in secondth area,
3) wet biomass is transferred to the second transition range of vapor blast area under extrusion,
Second transition range is in a chamber, on the one hand the chamber is separated with the multiple Dilvar zone, on the other hand with
The vapor blast area separates,
Second Dilvar zone and vapor blast area are separated by suppressing biomass plug, to make the total of the biomass
Solid content increases to 40 weight % or more, and the plug prevents liquid from flowing upwardly to second transition range from firstth area,
And
Second transition range is provided with the pipeline in extrusion process extracting the waste liquid separated with wet biomass out,
4) include the vapor blast area that the biomass is displaced through to the screw rod in following continuous area:
Biomass cooking zone is provided with the pipeline and vapor of the compacting biomass that conveying is generated by second transition range
Pipeline is injected,
The breathing space for expanding the biomass generated by the cooking zone,
The Disengagement zone that vapor is separated with biomass,
5) acid solution prepares area, is provided with
The pipeline that blast area is delivered to from the waste liquid extracted out in the second transition range and/or conveying are extracted out from the first Dilvar zone
Waste liquid pipeline,
The pipeline of transport acid and/or the pipeline for conveying water,
The acid solution of the preparation is recycled to the pipeline of first Dilvar zone,
Stirring system and optional heating device.
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
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| FR1656829 | 2016-07-18 | ||
| FR1656829A FR3053969B1 (en) | 2016-07-18 | 2016-07-18 | PROCESS OF TREATING LIGNOCELLULOSIC BIOMASS BY IMPREGNATION AND EXPLOSION WITH STEAM |
| PCT/EP2017/067468 WO2018015227A1 (en) | 2016-07-18 | 2017-07-11 | Method for treating lignocellulosic biomass by impregnation and steam explosion |
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| CN111788255A (en) * | 2017-12-20 | 2020-10-16 | Ifp 新能源公司 | Method for treating lignocellulosic biomass by impregnation |
| CN114717278A (en) * | 2021-01-06 | 2022-07-08 | 江南大学 | Agricultural and forestry biomass pretreatment method |
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| FR3075202B1 (en) * | 2017-12-20 | 2020-08-28 | Ifp Energies Now | LIGNO-CELLULOSIC BIOMASS TREATMENT PROCESS |
| WO2019215725A1 (en) * | 2018-05-08 | 2019-11-14 | We3 Solutions Inc. | Means and methods for converting waste biomass to saccharides and other downstream products |
| FR3090411B1 (en) | 2018-12-19 | 2020-12-25 | Ifp Energies Now | Radial tubular reactor |
| FR3090410B1 (en) | 2018-12-19 | 2020-12-25 | Ifp Energies Now | Tubular screw conveyor reactor |
| FR3090642B1 (en) | 2018-12-21 | 2020-12-25 | Ifp Energies Now | LIGNOCELLULOSIC BIOMASS TREATMENT PROCESS |
| FR3090423B1 (en) | 2018-12-21 | 2021-05-21 | Ifp Energies Now | PROCESS FOR CLEANING A LIGNOCELLULOSIC BIOMASS TREATMENT REACTOR |
| FR3090422B1 (en) | 2018-12-21 | 2021-05-21 | Ifp Energies Now | PROCESS FOR CLEANING A LIGNOCELLULOSIC BIOMASS TREATMENT REACTOR |
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| FR3113291A1 (en) | 2020-08-06 | 2022-02-11 | IFP Energies Nouvelles | Process for the production of alcohol by enzymatic hydrolysis and fermentation of lignocellulosic biomass |
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| CN111712531A (en) * | 2017-12-20 | 2020-09-25 | Ifp 新能源公司 | Lignocellulosic biomass processing method |
| CN111788255A (en) * | 2017-12-20 | 2020-10-16 | Ifp 新能源公司 | Method for treating lignocellulosic biomass by impregnation |
| CN111712531B (en) * | 2017-12-20 | 2022-04-15 | Ifp 新能源公司 | Lignocellulosic biomass processing method |
| CN111788255B (en) * | 2017-12-20 | 2022-07-08 | Ifp 新能源公司 | Method for treating lignocellulosic biomass by impregnation |
| CN114717278A (en) * | 2021-01-06 | 2022-07-08 | 江南大学 | Agricultural and forestry biomass pretreatment method |
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| ZA201808547B (en) | 2019-08-28 |
| JP7113002B2 (en) | 2022-08-04 |
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| DK3484945T3 (en) | 2020-08-24 |
| PT3484945T (en) | 2020-08-11 |
| FR3053969B1 (en) | 2019-12-20 |
| AU2017299081A1 (en) | 2019-01-17 |
| JP2019520830A (en) | 2019-07-25 |
| CA3030096A1 (en) | 2018-01-25 |
| EP3484945A1 (en) | 2019-05-22 |
| EP3484945B1 (en) | 2020-06-03 |
| US20190241984A1 (en) | 2019-08-08 |
| MY190660A (en) | 2022-05-09 |
| SI3484945T1 (en) | 2021-03-31 |
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| MX2019000320A (en) | 2019-07-04 |
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